3745-21-10
Compliance test methods and procedures.

[Comment: For dates of non-regulatory government publications,
publications of recognized organizations and associations, federal rules, and
federal statutory provisions referenced in this rule, see the last paragraph of
rule 3745-21-01 of the Administrative
Code titled"Incorporation by reference."]

(1)
The methods and procedures of this rule
apply to sources governed by rule
3745-21-09 of the Administrative
Code.

(2)
Use of an alternative
test method, in lieu of one of the USEPA's approved test methods or in lieu of
other methods specified in this rule, must be approved by the USEPA as a
revision of the state implementation plan.

(3)
The results of any compliance testing
required by the director for tests conducted pursuant to paragraphs (C) to (F)
and (L) of this rule shall not be accepted unless the Ohio EPA district office
or local air agency has been notified of the intent to test in accordance with
paragraph (A)(4) of this rule not less than thirty days before the proposed
initiation of the testing.

(4)
Any
person notifying the Ohio EPA district office or local air agency of a proposed
emissions compliance test shall include as part of the notification the
following information:

(a)
A statement
indicating the purpose of the proposed test and the applicable paragraph of
rule 3745-21-09 of the Administrative
Code;

(c)
Light, electricity, and other utilities
required for sample and data collection.

(B)
Method for the determination of volatile
organic compound content, solids content, and density of surface coatings and
inks.

(1)
This method applies to coatings,
inks or other coating materials employed in a coating line, printing line or
other operation. For purposes of this method "coating" shall also mean "ink" or
other coating material.

(2)
Any
determination of VOC content, solids content, or density of a coating shall be
based on the coating as employed (as applied), including the addition of any
thinner or viscosity reducer to the coating.

(3)
When a sample of a coating is obtained
for analysis by any of the procedures described in this method, the amount of
the sample shall be at least one quart. The sample shall be placed in an
air-tight container. When multiple package coatings are sampled, separate
samples of each component shall be obtained.

(4)
Using either the procedures set forth in
USEPA Method 24 (for coatings) and USEPA Method 24A (for flexographic and
rotogravure printing inks and related coatings), or the coating formulation
data from the coating manufacturer and coating user, the following shall be
determined, where appropriate:

Dc = density of coating, in pounds of coating per gallon of
coating.

Dvm = density of volatile matter in coating, in pounds of
volatile matter per gallon of volatile matter.

Vs = volume fraction of solids (nonvolatile matter) in coating,
in gallon of solids per gallon of coating.

Vvm = volume fraction of volatile matter in coating, in gallon
of volatile matter per gallon of coating.

Vw = volume fraction of water in coating, in gallon of water
per gallon of coating.

Ws = weight fraction of solids (nonvolatile matter) in coating,
in pound of solids per pound of coating.

Wvm = weight fraction of volatile matter in coating, in pound
of volatile matter per pound of coating. If this weight fraction is determined
by ASTM D2369-04, "Standard Test Method for Volatile Content of Coatings," the
drying conditions shall be one hundred ten degrees Celsius for one hour, except
where otherwise authorized by the director based on an alternate analytical
procedure that is satisfactorily demonstrated to the director by the coating
manufacturer to be more representative of the actual cure mechanism of the
coating.

Ww = weight fraction of water in coating, in pound of water per
pound of coating.

(5)
If
the coating contains a volatile matter other than VOC or water, the identity
and content of such volatile matter may be determined using either standard gas
chromatographic techniques or coating formulation data from the coating
manufacturer and coating user. The density of such volatile matter may be
determined using either the procedures set forth in ASTM D1475-98 or data from
reference texts. For purposes of this method, such volatile matter shall be
referred to as exempt solvent. The following may be determined, where
appropriate:

Des = density of exempt solvent, in pounds of exempt solvent
per gallon of exempt solvent.

Ves = volume fraction of exempt solvent in coating, in gallon
of exempt solvent per gallon of coating.

Wes = weight fraction of exempt solvent in coating, in pound of
exempt solvent per pound of coating.

(6)
The weight fraction Wvoc of VOC in a
coating and the volume fraction Vvoc of VOC in a coating shall be calculated as
follows, where appropriate:

(10)
The density of the VOC
content of a coating may be determined using either the procedures set forth in
ASTM D1475-98 or data from reference texts. If ASTM D1475-98 is employed, the
density shall be the arithmetic average of three determinations.

(11)
In the event of a dispute between
coating formulation data and data obtained by analytical procedures, the data
obtained by analytical procedures shall be employed, except as otherwise
provided in paragraph (B)(12) of this rule.

(12)
If a VOC content value obtained by
analytical procedures is higher than a VOC content value obtained by
formulation data due to any VOC that is formed during baking or curing (i.e.,
cure volatiles), then the VOC content of the portion of the coating not subject
to curing or baking shall be based on formulation data and the VOC content of
the portion of the coating subject to curing or baking shall be based on
analytical procedures. The portion of the coating subject to curing or baking
shall be equal to the measured transfer efficiency for the coating applicator
and object being coated. The approach described in this paragraph for
determining the VOC content of a coating may be used only when the applicable
VOC limitation is expressed in terms of pounds of VOC per gallon of deposited
solids and the transfer efficiency test method is specified in this rule or
rule 3745-21-09 of the Administrative
Code. Also, in cases where analytical results and formulation data are combined
for a waterborne coating, the interlaboratory precision adjustments specified
in the analytical procedures shall not be applied to the analytical results.

(1)
The provisions of
this paragraph are generally applicable to the test methods employed to
determine the VOC concentration and VOC mass emission rate for a gas stream or
exhaust vent and the collection or control efficiency for any control equipment
designed, installed, and operated for the purpose of reducing the emission of
VOC. For purposes of this paragraph, "vapor collection system" also means
capture system and "vapor control system" also means control system or control
device.

(2)
The concentration of
VOC in a gas stream or exhaust vent shall be determined by utilizing the
following methods:

(b)
USEPA Method 18) or
USEPA Method 25A, as appropriate, for sources specified in paragraphs
(O)(3)(c)(iv), (O)(4)(a)(ii), (CC) to (EE), and (LL) to (NN) [if the ppmv
compliance option in (LL), (MM) or (NN) is chosen] of rule
3745-21-09 of the Administrative
Code.

(3)
The following
procedures shall be included in any source testing or determination where
applicable:

(a)
The source shall be operated
at or near maximum operating capacity during any testing and the measurement of
the operating rate shall be made in a manner acceptable to the Ohio
environmental protection agency.

(b)
The VOC content of any coatings employed
shall be sampled and analyzed in accordance with paragraph (B) of this rule.

(c)
The capture efficiency of any
vapor collection system used to transport the VOC emissions from their point of
origin to the vapor control system shall be determined in accordance with USEPA
Methods 204 to 204F or the alternative capture efficiency testing protocols
specified in the USEPA, Office of Air Quality Planning and Standards document
entitled "Guidelines for Determining Capture Efficiency."

(d)
The control efficiency of any vapor
control system used to reduce the emission of VOC shall be based upon an
emissions test or a recovery test. For a vapor control system that destroys VOC
(e.g., an incineration system), either the streams entering and leaving the
vapor control system shall be tested or, if acceptable to the director, the
amount of VOC employed shall be measured and the gas stream leaving the vapor
control system shall be tested. For a vapor control system that recovers VOC
(e.g., a carbon adsorption system), either the gas streams entering and leaving
the vapor control system shall be tested or, if acceptable to the director, the
amounts of VOC employed and recovered or, employed and emitted, shall be
measured or tested.

(e)
For the
testing of a gas stream vented to a vapor control system, samples shall be
taken simultaneously at the inlet and the outlet of the vapor control system.

(g)
For gas streams tested by
USEPA Method 25 or 25A, the VOC emission rate shall be based upon the average
of three test runs. Each run shall have a minimum duration of one hour and a
minimum sample volume of .003 dry standard cubic meter, except that shorter
sampling times or smaller volumes, when necessitated by process variables, may
be found acceptable.

(h)
The
control efficiency of the vapor control system shall be the per cent reduction
in mass emissions of VOC between the inlet and the outlet of the vapor control
system. If this efficiency is based upon an emissions test utilizing USEPA
Method 25 or 25A, the mass emissions of VOC as carbon shall be employed in the
efficiency determination.

(i)
The
capture efficiency of the vapor collection system shall be the per cent of
total mass emissions of VOC emitted from the source which are vented to the
vapor control system. If this efficiency is based upon an emissions test
utilizing USEPA Method 25 or 25A, the mass emissions of VOC as carbon shall be
employed in the efficiency determination.

(j)
The overall control efficiency (in per
cent) of any control equipment for VOC emissions shall be the vapor capture
efficiency multiplied by the vapor control efficiency and divided by one
hundred.

(k)
The total mass
emission rate of VOC from a source equipped with control equipment shall be the
sum of VOC emissions from the vapor control system, VOC emissions not collected
by the vapor collection system and VOC emissions from any losses associated
with the vapor collection system and vapor control system.

(4)
The VOC mass emissions rate
for a gas stream tested by USEPA Method 18 shall be calculated as follows:

(6)
To convert a mass emission
rate from kilograms per hour to pounds per hour, multiply the mass emission
rate in kilograms per hour by 2.2046.

(7)
To convert a mass emission value from VOC
as carbon to VOC, divide the mass emission value of VOC as carbon by the weight
fraction of carbon in the average molecular weight of the VOC emission. The
determination of this weight fraction of carbon may be based on standard
analytical techniques or material formulation data.

(D)
Method for the determination of VOC
emissions from solvent metal cleaning:

(2)
The
purpose of this method is to quantify, by material balance, the amount of
solvent input into a degreaser over a sufficiently long period of time so that
an average emission rate can be computed.

(3)
The following procedure shall be followed
to perform a material balance test:

(b)
Record the amount of initial and make-up
solvent added to the tank with a flow meter or other means.

(c)
Record the type and amount or weight of
work load degreased each day.

(d)
At the end of the test run, pump out the used solvent and measure the amount
with a flow meter or other means. Also, estimate the volume of metal chips and
other material remaining in emptied sump, if significant.

(e)
Bottle a sample of the used solvent and
analyze it to find the per cent that is oil and other contaminants. The oil and
solvent proportions can be estimated by weighing samples of used solvent before
and after boiling off the solvent. Compute the volume of oils in the used
solvent. The volume of solvent displaced by this oil along with the volume of
make-up solvent added during operations is equal to the amount of VOC
emissions.

(4)
The
following procedure can be followed to perform a material balance test in lieu
of the procedure in paragraph (D)(3) of this rule:

(b)
Record the amount of initial
and make-up solvent added to the tank as measured with a flow meter or other
means.

(c)
Record the type and
amount or weight of work load degreased over the period of the test.

(d)
Record the amount of used solvent pumped
out of the tank for disposal as measured with a flow meter or other means.

(e)
Bottle a sample of the used
solvent and analyze it to find the per cent that is oil and other contaminants.

(f)
The VOC emissions from solvent
metal cleaning equals the total solvent added to the tank minus the solvent
contained in the used solvent being disposed.

(E)
Method for the determination of VOC
emissions from bulk gasoline terminals.

(1)
This method is applicable to determining the VOC emission rates at a bulk
gasoline terminal employing a vapor collection system and either a continuous
or intermittent vapor control system at a loading rack.

(2)
The VOC emission rates shall be
determined in accordance with the methods and procedures contained in
40 CFR
60.503(b), (c), (e) and (f)
of "Subpart XX - Standards of Performance for Bulk Gasoline Terminals," except
that the gasoline throughput during any test shall be not less than ninety per
cent of the maximum throughput of the loading rack(s) and not less than eighty
thousand gallons.

(3)
During any
test, all loading racks shall be open for each product line which is controlled
by the system under test. Simultaneous use of more than one loading rack shall
occur to the extent that such use would normally occur.

(4)
Simultaneous use of more than one
dispenser on each loading rack shall occur to the extent that such use would
normally occur.

(5)
Dispensing
rates shall be set at the maximum rate at which the equipment is typically
operated. Automatic product dispensers are to be used according to normal
operating practices.

(6)
Applicable operating parameters of the vapor control system shall be monitored
to demonstrate that the control unit is operating at design levels. Delivery
devices shall be leak free.

(7)
For each gasoline tank truck loaded during the test period, all potential
sources of leaks shall be checked in accordance with the method specified in
paragraph (K) of this rule. The tank identification number, the latest leak
check certification date, and the location and highest detector reading for
each incident of leakage shall be recorded.

(8)
During each test, all potential sources
of leaks in the vapor collection and control systems shall be monitored in
accordance with the method specified in paragraph (K) of this rule. The
location and highest detector reading for each incident of leakage shall be
recorded.

(F)
Method
for the detection of leaks of VOC from petroleum refinery equipment and organic
chemical manufacturing equipment.

(1)
This
method is applicable to the detection of leaks of VOC into the ambient air from
petroleum refinery equipment and any chemical manufacturing equipment subject
to paragraph (T) or (DD) of rule
3745-21-09 of the Administrative
Code.

(2)
The detection of leaks
shall be determined in accordance with the test procedure set forth in USEPA
Method 21.

(a)
Zero air, which consists
of less than ten ppmv of hydrocarbon in air; and

(b)
A mixture of air and methane or n-hexane
at a concentration of approximately, but less than, ten thousand ppmv of
methane or n-hexane.

(4)
The leak detection instrument shall be
calibrated before use on each day of its use.

(G)
Standard method for the determination of
the leak tightness of gasoline tank trucks (method G).

(1)
This method is applicable to determining
the leak tightness of gasoline tank trucks which are equipped with piping,
hoses and other devices for the collection or return of gasoline vapors during
the transfer of gasoline at a gasoline dispensing facility, bulk gasoline plant
or bulk gasoline terminal.

(2)
The
leak tightness of a gasoline tank truck shall be determined in accordance with
the test procedure set forth in USEPA Method 27. For the pressure test, the
initial pressure shall be 18.0 inches of water. For the vacuum test, the
initial vacuum shall be 6.0 inches of water.

(3)
If any gasoline tank truck or compartment
of a gasoline tank truck sustains either a pressure decrease greater than 3.0
inches of water over five consecutive minutes for the pressure test or a
pressure increase greater than 3.0 inches of water over five consecutive
minutes for the vacuum test, the tank truck is not leak tight. If not leak
tight, repair the tank truck as necessary and repeat the entire test procedure
specified in paragraph (G)(2) of this rule until the gasoline tank truck or
compartment passes the test.

(I)
Method for the determination of seal gaps
in an external floating roof tank.

(1)
This
method is applicable to determining the width and area of any gaps between the
wall of an external floating roof tank and a seal which is around the
circumference of the external floating roof.

(2)
The width of any seal gap is the distance
between the seal and the tank wall. It is determined by using probes of various
widths to accurately measure the actual distance from the seal to the tank
wall.

(3)
The area of any seal gap
is determined by multiplying the width of the seal gap, as determined in
paragraph (I)(2) of this rule, by the circumferential length of the gap.

(4)
The total seal gap area is the
accumulated area of all gaps which are greater than 0.125 inch in width.

(J)
Method for the
determination of the perchloroethylene content of wastes at a dry cleaning
facility which uses perchloroethylene.

(1)
The method is applicable to determining the perchloroethylene content in per
cent by weight for waste at a dry cleaning facility from any distillation
operation which distills perchloroethylene and from any diatomaceous earth
filter which filters perchloroethylene.

(2)
The perchloroethylene content of the
waste in per cent by volume is determined in accordance with the procedure in
ASTM D322-97(2002)e1, and is calculated as the diluent content in that
procedure.

(3)
The density of the
waste is determined by weighing a known volume of the waste and is calculated
as the net weight of the waste in pounds divided by the volume of the waste in
gallons.

(4)
The perchloroethylene
content of the waste in per cent by weight is calculated as the product of its
diluent content and 13.55, divided by its density.

(b)
Gasoline
barges and gasoline tank trucks during loading, providing the vapor control
system, vapor collection system, or vapor balance system which is connected to
the gasoline barge or gasoline tank truck does not create a back pressure
greater than eighteen inches of water gauge pressure.

(2)
This method describes the procedures to
be followed for detecting leaks of gasoline vapors by means of a portable
hydrocarbon gas analyzer, which is calibrated to read in per cent of the lower
explosive limit as propane.

(iii)
Has a minimum range of zero to one
hundred per cent of the lower explosive limit as propane; and

(iv)
Has a response time for full-scale
deflection of less than eight seconds with sampling line and probe attached.

(4)
The
portable hydrocarbon gas analyzer is calibrated with 2.2 per cent propane by
volume in air (or equivalent calibration gas) for one hundred per cent of the
lower explosive limit according to the procedures and frequency specified by
the manufacturer.

(a)
Connect the liquid manometer to a
pressure tap in the vapor control system, vapor collection system, or vapor
balance system as close as possible to the connection with the gasoline barge
or gasoline tank truck;

(b)
Record
the pressure periodically during loading of the gasoline barge or gasoline tank
truck;

(c)
Check with the portable
hydrocarbon gas analyzer all potential leak sources on the gasoline barge or
gasoline tank truck during loading and on the vapor control system, vapor
collection system, or vapor balance system by:

(i)
Maintaining the probe's inlet about one
inch from the potential leak source in the path of (parallel to) the vapor flow
from a leak;

(ii)
Moving the probe
slowly around the periphery of the potential leak source to locate the point of
highest meter response;

(iii)
Blocking as much as possible the wind from the area being monitored; and

(d)
Record the location
of leakage and the highest detector reading for each incidence of leakage.

(L)
Method
for the determination of the emission of volatile organic compounds from a
dryer at a petroleum dry cleaning facility.

(1)
This method is applicable to determining
the volatile organic compound emission rate of a dryer containing articles
cleaned in petroleum solvent at a dry cleaning facility.

(2)
The dryer shall be tested under normal
operating conditions for at least thirty dryer loads that total not less than
four thousand pounds dry weight of articles cleaned. The dryer loads shall
represent a normal range of variations in fabrics, solvents, load weights,
temperatures, flow rates, and process deviations. Each dryer load shall be
tested in accordance with paragraph (L)(3) or (L)(4) of this rule.

(3)
For each dryer load the following shall
be conducted and recorded:

(b)
Determine the average organic
concentration C in the stack (in ppmv as propane) in accordance with USEPA
Method 25A in which the flame ionization analyzer is calibrated with propane
standards.

(c)
Determine the ratio
R of the flame ionization analyzer's response to a given parts per million by
volume concentration of propane to its response to the same parts per million
by volume concentration of the volatile organic compounds present in the stack
gas.

(d)
Determine the molecular
weight M (in pounds per pound-mole) of the volatile organic compounds present
in the stack gas. Such determination shall be based on data from the
manufacturer of the cleaning solvent or on standard analytical techniques.

(e)
Measure and record the weight
Wa (in pounds dry weight) of the articles to be cleaned.

(f)
Calculate the weight Wvoc (in pounds) of
the volatile organic compounds emitted into the ambient air using the following
equation:

Wvoc = V X C X R X M

(4)
For each dryer load the following shall
be conducted and recorded:

(a)
All weights
shall be measured to the nearest 0.5 pound or less on a scale that is accurate
to 0.5 pound at weights of up to two hundred pounds.

(b)
Measure and record the weight Wa (in
pounds) of the articles to be cleaned.

(c)
Measure and record the initial weight Wi
(in pounds) of the articles to be dried after the washing cycle.

(d)
Measure and record the final weight Wf
(in pounds) of the articles removed from the dryer after the drying cycle.

(e)
Measure and record the weight
Wr (in pounds) of any recovered liquid materials.

(f)
Calculate the weight Wvoc (in pounds) of
the volatile organic compounds emitted into the ambient air using the following
equation:

Wvoc = Wi - Wf - Wr

(5)
The dryer's volatile organic compound
emission rate (in pounds per one hundred pounds dry weight of articles cleaned)
shall be calculated for the combined dryer loads tested under this method as
equal to one hundred multiplied by the sum total of Wvoc and divided by the sum
total of Wa.

(M)
Method
for the determination of the amount of volatile organic compounds contained in
filtration waste at a petroleum dry cleaning facility.

(1)
This method is applicable to determining
the amount of volatile organic compounds contained in the waste from a solvent
filter used to filter petroleum solvent at a dry cleaning facility.

(2)
The solvent filter shall be tested under
normal operating conditions for at least three time periods according to the
procedures specified in paragraph (M)(3) of this rule.

(N)
Method for the
determination of the length of time to operate the recovery cycle of a solvent
recovery dryer at a petroleum dry cleaning facility.

(1)
This method is applicable to determining
the length of time for operating the solvent recovery cycle of a solvent
recovery dryer at a petroleum dry cleaning facility in order to assure that the
flow rate of recovered petroleum solvent at the termination of solvent recovery
cycle is no greater than fifty milliliters per minute.

(2)
The dryer shall be tested under normal
operating conditions for a duration of no less than two weeks during which no
less than one-half of the dryer loads shall be monitored for their final
recovered solvent flow rate.

(3)
The suggested point for measuring the flow rate of recovered solvent is from
the outlet of the solvent-water separator. Near the end of the recovery cycle,
the entire flow of recovered solvent is diverted to a graduated cylinder. As
the recovered solvent collects in the graduated cylinder, the elapsed time is
monitored and recorded in periods greater than or equal to one minute. At the
same time, the volume of solvent in the graduated cylinder is monitored and
recorded to determine the volume of recovered solvent that is collected during
each time period. The recovered solvent flow rate is calculated by dividing the
volume of solvent collected per period by the length of time elapsed during the
period and converting the result with appropriate factors into units of
milliliters per minute. The recovery cycle and the monitoring procedure is
continued until the flow rate of solvent is less than or equal to fifty
milliliters per minute. The date, the type of articles cleaned, and the total
length of the recovery cycle shall be recorded for each dryer load being
monitored.

(O)
Method
for the determination of equipment in VOC service and in light liquid service.

(1)
This method is applicable to equipment at
a petroleum refinery or a process unit subject to paragraph (T) or (DD) of rule
3745-21-09 of the Administrative
Code.

(2)
Any piece of equipment
is presumed to be in VOC service, unless the owner or operator demonstrates
that the piece of equipment is not in VOC service according to the following
provisions:

(a)
The piece of equipment is
considered not in VOC service if it can be determined that the VOC content of
the process fluid, which is contained in or contacts the piece of equipment,
can be reasonably expected never to exceed ten per cent by weight.

(b)
For purposes of determining the VOC
content of a process fluid, procedures that conform to the general methods
described in ASTM E168-99(2004), ASTM E169-04, and ASTM E 260-73 shall be used.

(c)
The owner or operator may use
engineering judgment rather than the procedures contained in paragraph
(O)(2)(b) of this rule to demonstrate that the VOC content of a process fluid
does not exceed ten per cent by weight, provided the VOC content clearly does
not exceed ten per cent by weight. In the event the Ohio EPA or the USEPA has a
disagreement with an engineering judgment, paragraph (O)(2)(b) of this rule
shall be used to resolve the disagreement.

(3)
A piece of equipment is in light liquid
service if it contains or is in contact with a process fluid that meets all of
the following conditions:

(b)
The vapor pressure of one or more of the
pure components within the process fluid is greater than 0.04 pound per square
inch at sixty-eight degrees Fahrenheit. Vapor pressures may be obtained from
standard reference texts or may be determined by the method in ASTM D 2879-70.

(c)
The total concentration of the
pure components having a vapor pressure greater than 0.04 pound per square inch
at sixty-eight degrees Fahrenheit is equal to or greater than twenty per cent
by weight.

(P)
Method for the determination of the net
heating value of a gas, the actual exit velocity for a flare, and the maximum
permitted velocity for an air-assisted flare.

(3)
The actual exit velocity of a
flare shall be calculated by dividing the volumetric flow rate (in units of
standard temperature and pressure) of the flare header or headers that feed the
flare, as determined by USEPA Methods 2, 2A, 2C, or 2D as appropriate, by the
unobstructed (free) cross-sectional area of the flare tip, as determined by
design and engineering principles.

(4)
The maximum permitted velocity of an
air-assisted flare shall be determined by the following equation:

(5)
To express the net heating
value of a gas in Btu per standard cubic foot, multiply Ht by 26.84.

(6)
To express a velocity in feet per second,
multiply the velocity in meters per second by 3.281.

(Q)
Method for the detection of leaks of
gasoline vapors from a vapor control system installed at a gasoline dispensing
facility (static leak test).

(1)
This method
is applicable to quantifying the vapor tightness of a vapor balance system or a
vacuum assist control system installed at a gasoline facility.

(2)
This method describes the procedures to
be followed for detecting leaks of gasoline vapors by pressurizing the entire
vapor recovery control system to two inches of water column and then allowing
the system pressure to decay for five minutes. The acceptability of the final
pressure is based upon the vapor system volume or ullage space. The allowable
five minute final pressure is based upon the gasoline tank ullage, pressure
decay equations, and the number of affected nozzles.

(3)
The equipment, procedures, and pressure
decay leak criteria are specified in appendix A of this rule.

(R)
Method for the determination
of the dynamic pressure performance for a vapor control system installed at a
gasoline dispensing facility (dynamic pressure performance test).

(1)
This method is applicable to determining
the dynamic pressure at known dispensing flow rates for a vapor control system
installed at a gasoline dispensing facility. This method is used to quantify
the back pressure and detect liquid obstructions in the vapor path leading from
the dispensing nozzle to the gasoline storage tank.

(2)
This method describes the procedures to
be followed in simulating the dynamic back pressures associated with known
gasoline dispensing rates and liquid blockages by passing nitrogen through the
vapor control system at three flow rates after liquid gasoline has been
introduced into the vapor return piping.

(3)
The equipment, procedures, and dynamic
pressure performance criteria are identified in appendix B of this rule.

1.1 This test procedure is used to quantify the
vapor tightness of vapor control systems installed at any gasoline dispensing
facility (GDF) equipped with pressure/vacuum (P/V) valves, provided that the
designed pressure setting of the P/V valves is a minimum of 2.5 inches of water
column (inches H2O). Excessive leaks in the vapor control system will increase
the quantity of fugitive hydrocarbon emissions and lower the overall
efficiencies of both the Stage I and Stage II vapor control systems.

1.2 For those systems equipped with a P/V valve(s)
allowed to have a designed cracking pressure less than 2.5 inches H2O, the
valve(s) shall be bagged to eliminate, from the test results, any flow
contribution through the valve assembly. The valve/vent pipe connection,
however, shall remain unobstructed during this test.

1.3 For those facilities not required to be
equipped with a P/V valve(s), the vent pipe(s) shall be capped. For these
installations, the test may be conducted at the vent pipe(s).

2.1 The entire vapor control system is pressurized
with nitrogen to two ( 2.0 ) inches H2O. The system pressure is then allowed to
decay and the pressure after five (5) minutes is compared with an allowable
value. The minimum allowable five-minute final pressure is based on the system
ullage and pressure decay equations. For the purpose of compliance
determination, this test shall be conducted after all back-filling, paving, and
installation of all Stage I and Stage II components, including P/V valves, has
been completed.

2.2 For a GDF equipped with a coaxial Stage I
system this test shall be conducted at a Stage II vapor riser. For a GDF which
utilizes a two-point Stage I system this test shall be conducted at the Stage I
vapor coupler, provided that the criteria set forth in Section 6.7 have been
met. If the integrity criteria for two-point systems specified in Section 6.7
are met, this test shall be conducted at the Stage I vapor coupler unless the
vapor control system possesses a design which is incompatible with testing at
this location.

3.1 If mechanical pressure gauges are employed,
the full-scale range of the pressure gauges shall be 0- 2.0, 0- 1.0, and 0-
0.50 inches H2O column. Maximum incremental graduations of the pressure gauge
shall be 0.05 inches H2O and the minimum accuracy of the gauge shall be three
percent of full scale. The minimum diameter of the pressure gauge face shall be
4 inches.

3.2 If an electronic pressure measuring device is
used, the full-scale range of the device shall not exceed 0-10 inches H2O with
a minimum accuracy of 0.5 percent of full-scale. A 0-20 inches H2O device may
be used, provided the equivalent accuracy is not less than 0.25 percent of full
scale.

3.3 The minimum ullage during the test shall be 25
percent of the tank capacity (total of alltanks if manifolded) or
500 gallons, whichever is greater. The maximum total ullage shall be 25,000
gallons. These values are exclusive of all vapor piping volumes.

3.4 The minimum and maximum nitrogen feed-rates,
into the system, shall be one (1) and five (5) CFM, respectively.

4.1 Nitrogen shall not be introduced into the
system at flowrates exceeding five (5) CFM as this may bias the results of the
test toward non-compliance.

4.2 For vacuum-assist Stage II systems which
utilize an incinerator, power to the collection unit shall be turned off during
testing.

4.3 For vacuum-assist systems which locate the
vacuum producing device in-line, between the Stage II vapor riser and the
storage tank, the following shall apply:

4.3.1 A valve shall be installed at the vacuum
producing device. When closed, this valve shall isolate the vapor passage
downstream of the vacuum producing device.

4.3.2 The storage tank side of the vacuum
producing device shall be tested in accordance with the procedures outlined in
Section 7 of this method. Compliance shall be determined by comparing the final
five-minute pressure with the allowable minimum five-minute final pressure from
the first column (1-6 affected nozzles) in Table IB or use the corresponding
equation in Section 9.2.

4.3.3 The upstream vapor passage (nozzle to vacuum
producing device) shall also be tested. Methodology for this test shall be
submitted to the Ohio EPA, Division of Air Pollution Control for approval prior
to submission of test results or shall be conducted in accordance with the
procedures set forth in the applicable CARB
certification.

5.1 Nitrogen. Use commercial grade nitrogen in a
high pressure cylinder, equipped with a two-stage pressure regulator and a one
psig pressure relief valve. A one psig (maximum) pressure relief valve is
required and mustbe present. In addition, the cylinder of nitrogen
mustbe grounded.

5.2 Pressure Measuring Device. Use 0- 2.0, 0- 1.0,
and 0- 0.50 inches H2O pressure gauges connected in parallel, a 0-2 inches H2O
manometer, or an electronic pressure measuring device to monitor the pressure
decay in the vapor control system. The pressure measuring device shall, at a
minimum, be readable to the 0.05 inches H2O.

5.4 Vapor Coupler Integrity Assembly. Assemble OPW
633-A, 633-B, and 634-A adapters, or equivalent, as shown in Figure 2 below. If
the test is to be conducted at the storage tank Stage I vapor coupler, this
assembly shall be used prior to conducting the static leak test in order to
verify the pressure integrity of the vapor poppet. The internal volume of this
assembly shall not exceed 0.1 cubic feet.

5.5 Vapor Coupler Test Assembly. Use a compatible
OPW 634-B cap, or equivalent, equipped with a center probe to open the poppet,
the appropriate pressure measuring device to monitor the pressure decay, and a
connection for the introduction of nitrogen into the system. See Figure 3 below
for example.

5.7 Flowmeter. Use a Dwyer flowmeter, Model
RMC-104, or equivalent, to determine the required pressure setting of the
delivery pressure gauge on the nitrogen supply pressure regulator. This
pressure shall be set such that the nitrogen flowrate is between 1.0 and 5.0
CFM.

5.8 Combustible Gas Detector. A Bacharach
Instrument Company, Model 0023-7356, or equivalent, may be used to verify the
pressure integrity of system components during this test.

5.9 Leak Detection Solution. Any liquid solution
designed to detect vapor leaks may be used to verify the pressure integrity of
system components during this test.

6.1.2 A one psig relief valve shall be installed
to prevent the possible over-pressurizing of the storage tank.

6.2 Product dispensing shall not occur during the
test. There shall have been no Stage I deliveries into or out of the storage
tanks within the three hours prior to the test. For vacuum-assist Stage II
systems, product dispensing shall not occur during the thirty minutes
immediately prior to the test.

6.3 Measure the gallons of gasoline present in
each underground storage tank and determine the actual capacity of each storage
tank from facility records. Calculate the ullage space for each tank by
subtracting the gasoline gallonage present from the actual tank capacity. The
minimum ullage during the test shall be 25 percent of the tank capacity (total
of alltanks if manifolded) or 500 gallons, whichever is greater.
The total ullage shall not exceed 25,000 gallons.

6.4 For two-point Stage I systems, this test shall
be conducted with the dust cap removed from the vapor coupler. This is
necessary to determine the vapor tightness of the Stage I vapor poppet. See
Section 6.7 if this test is to be conducted at the Stage I vapor coupler.

6.4.1 For coaxial Stage I systems this test shall
be conducted with the dust cap removed from the Stage I coupler. This is
necessary to insure the vapor tightness of the Stage I vapor poppet.

6.4.2 Verify that the liquid level in the storage
tank is at least four (4) inches above the highest opening at the bottom of the
submerged drop tube.

6.5 If the Stage I containment box is equipped
with a drain valve, the valve assembly may be cleaned and lubricated prior to
the test. This test shall, however, be conducted with the drain valve installed
and the manhole cover removed. See subsection 7.4.1 for further details
regarding containment box drain valves.

6.6 If the test is to be conducted at a Stage II
vapor riser, disconnect the dispenser end of one vapor control hose and install
the "T" connector assembly (see Figure 1). Connect the nitrogen gas supply (do
not use air) and the pressure measuring device to the "T" connector.

6.6.1 For those Stage II systems utilizing a
dispenser mounted remote vapor check valve, the "T" connector assembly shall be
installed on the vapor riser side of the check valve.

6.7 If this test is to be conducted at the Stage I
vapor coupler on a two-point Stage I system, the procedures set forth in
subsections 6.7.1 and 6.7.2 shall be successfully completed prior to testing.
The static leak test shall not be conducted at the Stage I coupler at
facilities equipped with coaxial Stage I systems.

6.7.1 Connect the Vapor Coupler Integrity Assembly
to the Stage I vapor coupler. Connect the Vapor Coupler Test Assembly. Connect
the nitrogen supply to the assembly and carefully pressurize the internal
volume of the assembly to two ( 2.0 ) inches H2O. Start the stopwatch. Record
the final pressure after one minute.

6.7.2 If the pressure after one minute is less
than 0.25 inches H2O, the leak rate through the Stage I vapor poppet precludes
conducting the static leak test at this location. Repair or replace the faulty
component(s) as necessary and restart the test pursuant to Section 6.7.1. If
the pressure after one minute is greater than or equal to 0.25 inches H2O, the
static leak test may be conducted at this location. This criteria assures a
maximum leak rate through the Stage I vapor poppet of less than 0.0004 cubic
feet per minute.

6.7.3 Disconnect the Vapor Coupler Integrity
Assembly from the Stage I vapor coupler. If the requirements of subsection
6.7.2 were met, install the Vapor Coupler Test Assembly to the Stage I vapor
coupler.

6.8 All pressure measuring device(s) shall be
bench calibrated using either a reference gauge or incline manometer.
Calibration shall be performed at 20, 50, and 80 percent of full scale.
Accuracy shall be within two percent at each of these calibration points.
Calibrations shall be conducted on a frequency not to exceed 90 days. The
individual conducting the test shall supply to the Ohio EPA or its designated
local air agency with proof of equipment calibration meeting the requirements
of this Section.

6.9 Use the flowmeter to determine the nitrogen
regulator delivery pressures which correspond to nitrogen flowrates of 1.0 and
5.0 CFM. These pressures define the allowable range of delivery pressures
acceptable for this test procedure. Also record which regulator delivery
pressure setting, and the corresponding nitrogen flowrate, will be used during
the test.

6.10 Use Equation 9.3 to calculate the approximate
time required to pressurize the system ullage to the initial starting pressure
of two ( 2.0 ) inches H2O. This will allow the tester to minimize the quantity
of nitrogen introduced into those systems which cannot comply with the static
leak standards.

6.11 Attach the Vapor Coupler Test assembly to the
Stage I poppet or the "T" connector assembly to the Stage II vapor riser. Read
the initial pressure of the storage tank and underground piping. If the initial
pressure is greater than 0.5 inches H2O, carefully bleed off the pressure, in
accordance with all applicable safety procedures, in the storage tank and
underground piping to less than 0.5 inches H2O column.

7.1 Open the nitrogen gas supply valve and set the
regulator delivery pressure within the allowable range determined in Section
6.9, and start the stopwatch. Pressurize the vapor system (or subsystem for
individual vapor return line systems) to at least2.2 inches H2O
initial pressure. It is critical to maintain the nitrogen flow until the
pressure stabilizes, indicating temperature and vapor pressure stabilization in
the tanks. Check the test equipment using leak detecting solution or a
combustible gas detector to verify that all test equipment is leak tight.

7.1.1 If the time required to achieve the initial
pressure of two ( 2.0 ) inches H2O exceeds twice the time derived from Equation
9.3, stop the test and use liquid leak detector, or a combustible gas detector,
to find the leak(s) in the system. Repair or replace the faulty component(s)
and restart the test pursuant to Section 7.1.

7.2 Close and disconnect the nitrogen supply.
Start the stopwatch when the pressure has decreased to the initial starting
pressure of two ( 2.0 ) inches H2O.

7.3 At one-minute intervals during the test,
record the system pressure. After five minutes, record the final system
pressure. See the applicable of Table IA (or Equation 9.1 ) or IB (or Equation
9.2 ) to determine the acceptability of the final system static pressure
results. For intermediate values of ullage in Table IA and IB, linear
interpolation may be employed.

7.4 If the system failed to meet the criteria set
forth in Table I (or the appropriate equation in Section 9), repressurize the
system and check all accessible vapor connections using leak detector solution
or a combustible gas detector. If vapor leaks in the system are encountered,
repair or replace the defective component and repeat the test. Potential
sources of leaks include nozzle check valves, pressure/vacuum reliefvalves,
containment box drain valve assemblies, and plumbing connections at the risers.

7.4.1 If the facility fails to comply with the
static leak test standards and the Stage I system utilizes a non-CARB-certified
drain valve equipped containment box, which was installed prior to July 1,
1992, for which a CARB-certified replacement drain valve assembly is not
marketed, the following two subsections shall apply:

7.4. 1.1 The drain valve may be removed and the
port plugged. Retest the system. If the facility complies with the static leak
test standards under these conditions, the facility shall be considered
complying with the requirements, provided that the manufacturer and model
number of the containment box and the date of installation are submitted with
the test results.

7.4. 1.2 The criteria set forth in subsection
7.4. 1.1 shall not apply after July 1, 1996.

7.5 After the remaining system pressure has been
relieved, remove the Vapor Coupler Test Assembly or "T" connector assembly and
reconnect the vapor control hose, if applicable.

7.6 If the vapor control system utilizes
individual vapor return lines, repeat the leak test for each gasoline grade.
Avoid leaving any vapor return line open longer than is necessary to install or
remove the "T" connector assembly.

8.1 Use the applicable of Table IA or IB, or the
applicable of Equations 9.1 or 9.2, to determine the compliance status of the
facility by comparing the final five-minute pressure with the minimum allowable
final pressure.

8.1.1 For balance Stage II systems use Table IA or
the applicable of Equation 9.1 to determine compliance.

8.1.2 For vacuum-assist Stage II systems use Table
IB or the applicable of Equation 9.2 to determine compliance.

10.1 The calculated ullage and system pressures
for each five-minute vapor control system test shall be reported as shown in
Form 1. Be sure to include the Stage I system type (two-point or coaxial), the
Stage II system type, whether the system is manifolded, and the one-minute
pressures during the test. The tester may either provide all information listed
in Form 1 in the comprehensive test report or include a copy of this form along
with the comprehensive written report.

1.1 This procedure is used to verify compliance
with the applicable dynamic back pressure limits imposed on any Stage II vapor
control system. The applicability of the following Alternate Methods is
dependent upon the regulatory requirements imposed by the CARB
certification.

1.1.1 Alternate Method 1.This procedure is
applicable if the dynamic back pressure standards are imposed from the nozzle
to the gasoline storage tank, provided remote vapor check valves are not part
of the Stage II system.

1.1.2 Alternate Method 2.This procedure is
applicable if the dynamic back pressure standards are imposed from the Stage II
riser to the gasoline storage tank, provided there is no vacuum-producing
device located between the riser and tank.

1.1.3 Alternate Method 3.This procedure is
applicable if the dynamic back pressure standards are imposed at the
nozzle/vehicle interface during vehicle fueling.

1.1.4 Alternate Method 4.This procedure shall be
conducted, in conjunction with the applicable of Alternate Methods 1, 2, or 3
if the Stage II system utilizes an incinerator.

1.2 Alternate Methods 1 and 2 shall be conducted
with the Stage I vapor poppet open.Alternate Methods 3 and 4 shall
be conducted with the poppet closed.

1.3 Other Alternate Methods may be used provided
that written approval has been granted by the Ohio EPA, Division of Air
Pollution Control. Such approval shall be based upon demonstrated equivalency
of any proposed methodology.

2.1 Using Alternate Methods 1, 2, or 4, the
dynamic back pressure during vehicle fueling is simulated by passing nitrogen
through the Stage II vapor control system at specified rates. The resultant
dynamic back pressure is measured using a pressure gauge, or equivalent device.
Alternate Method 3 is a direct measurement of the pressure at the
nozzle/fillpipe interface during gasoline dispensing. Liquidblockages in the
vapor return lines are also detected using these Methods.

3.1 The minimum and maximum dynamic back pressures
that can be measured are dependent upon the range of the pressure gauges used.
Required gauge ranges are as follows:

3.1.1 Alternate Method 1. 0- 0.5 and 0-2 inches
H20.

3.1.2 Alternate Method 2. 0- 0.25, 0-1, and 0-2
inches H2O.

3.1.3 Alternate Method 3. - 1.0 -+ 1.0 inches H2O.

3.1.4 Alternate Method 4. 0- 0.5 and 0-1 inches
H2O.

3.2 If mechanical pressure gauges are employed,
the minimum diameter of the gauge face shall be four inches, and the minimum
accuracy of the gauge shall be three percent of full scale.

3.3 If an electronic pressure measuring device is
used, the full-scale range of the device shall not shall not exceed 0-10 inches
H2O with a minimum accuracy of 0.5 percent of full scale. A 0-20 inches H2O
device may be used provided that the equivalent accuracy is not less than 0.25
percent of full-scale.

5.1 Nitrogen High Pressure Cylinder with Pressure
Regulator. Use a high pressure nitrogen cylinder capable of maintaining a
pressure of 2000 psig and equipped with a compatible two-stage pressure
regulator and a one psig relief valve. The nitrogen cylinder
mustbe grounded and the one psig (maximum) relief valve
mustbe present during the test.

5.2 Rotameter. Use a calibrated rotameter capable
of accurately measuring nitrogen flowrate(s) applicable for the imposed dynamic
back pressure limits.

5.3 Pressure Gauges. Use differential pressure
gauges, or equivalent, as specified in the applicable subsection of Section
3.1.

5.4 Automobile fillpipe. Use an automobile
fillpipe, if applicable, known to be compatible with all bellows-equipped vapor
control nozzles, and equipped with a pressure tap. See Figure 1.

5.5 Nitrogen. Use commercial grade nitrogen.

5.6 Hand Pump. Use a gasoline compatible hand
pump, if applicable, to drain any gasoline from condensate pots.

5.7 Stopwatch. For Alternate Method 3, use a
stopwatch, or equivalent, accurate to within 0.5 seconds.

6.1 Alternate Method 1.The following subsections
are applicable for those Stage II systems where a limitation is imposed on the
dynamic back pressure between the nozzle and the gasoline storage tank,
provided that remote vapor check valves are not employed. For those Stage II
systems which do notutilize a remote vapor check valve, assemble
the apparatus as shown in Figure 1, ensuring that the riser shut-off valve on
the test equipment is closed. If a Hirt Stage II system is used, the vacuum
producing device shall be turned off during this test.

6.1.2 The test equipment mustbe
leak-checked prior to use. Plug the nozzle end of the auto fillpipe and open
the nitrogen cylinder. Adjust the flow meter control valve until a pressure of
50 percent of full scale is indicated on the high range pressure gauge. Close
the nitrogen cylinder valve and any toggle valves. A pressure decay of less
than 0.2 inches H2O, in five minutes, is considered acceptable.

6.1.3 Perform an initial visual examination for
vapor leaks at the nozzles and hoses of the Stage II system to be tested. All
leak sources shall be repaired or the component(s) removed and replaced prior
to testing.

6.1.4 The Stage I vapor poppet shall be propped
open in such a manner that the valve is not damaged. This may be accomplished
using a Dynamic Pressure Release Assembly as shown in Figure 2.

6.1.5 Pour a minimum of two (2) gallons of
gasoline into each and every Stage II vapor return riser. This gasoline may be
introduced into the Stage II riser in any appropriate manner. Alternatively, a
minimum of twenty gallons of gasoline may be introduced into the Stage II riser
furthest from the gasoline storage tank, provided that the riser is common to
all products available at that dispenser. If product-specific risers are
employed, a minimum of seven gallons, per product grade, may be introduced into
the riser of each product which is furthest from the gasoline storage tank.

7.1 Alternate Method 1.Insert the nozzle into the
fillpipe of the Dynamic Pressure Performance Test Unit as shown in Figure 1
below, ensuring that a tight seal at the fillpipe/nozzle interface is achieved.

7.1.1 Connect the nitrogen supply to the test
assembly.

7.1.2 Open the nitrogen supply, set the delivery
pressure to 5 psig, and use the flowmeter control valve to adjust the flowrate
to lowest of the required nitrogen flowrates.

7.1.3 A pulsating gauge needle indicates nitrogen
passing through a liquid obstruction in the vapor return system. Close the flow
meter control valve, redrain the nozzle and hose assembly, and repeat the test.
If this condition re-occurs, the cause of the liquid trap in the system must be
corrected.

7.2 Alternate Method 2.Those Stage II systems
subject to regulatory limitations on the dynamic back pressure between the
Stage II riser and gasoline storage tank shall be tested using this
methodology.

Specified nitrogen flowrates and associated maximum allowable
Dynamic Backpressures are included in Form 2.

7.2.6 Repeat subsections 7.2.3 through 7.2.5 at
all required nitrogen flowrates for each and every riser.

7.3 Alternate Method 3.Those bellows-equipped
Stage II systems subject to regulatory limitations on the dynamic back pressure
at the nozzle/fillpipe interface during gasoline dispensing shall use the
following methodology.

7.3.4 Activate the dispenser, set the nozzle
hold-open latch on low, and after at least one gallon has been dispensed start
the stopwatch. Dispense a minimum of four gallons of gasoline.

Use the stopwatch to accurately time the dispensing rate.
Record the total gallons dispensed and calculate the flow rate in gallons per
minute. The following data shall be recorded on the field data sheet as shown
in Form 3:

7.3.5 This Alternate Method shall only be
conducted with the Stage I vapor poppet closed, since gasoline is being
dispensed during the test.

7.4 Alternate Method 4.Those Stage II systems
which utilize an incinerator shall conduct this test in conjunction with the
applicable of Alternate Method 1, 2, or 3. This procedure verifies proper
drainage of gasoline from the base of the vent pipe to the gasoline storage
tank.

7.4.1 After verifying compliance with the dynamic
back pressure standards, pursuant to the applicable of Alternate Methods 1, 2,
or 3, close the Stage I vapor poppet.

7.4.2 Remove the pressure/vacuum (P/V) valve(s)
from each vent pipe.

7.4.3 Carefully pour a minimum of five gallons of
gasoline down each vent pipe.

7.4.4 Install the Vent Pipe Pressure Assembly as
shown in Figure 5 below. Open the Stage I poppet(s) on all affected tanks.